WO2012005545A2 - Procédé pour l'extraction économique de lithium à partir d'une solution comprenant du lithium - Google Patents
Procédé pour l'extraction économique de lithium à partir d'une solution comprenant du lithium Download PDFInfo
- Publication number
- WO2012005545A2 WO2012005545A2 PCT/KR2011/005026 KR2011005026W WO2012005545A2 WO 2012005545 A2 WO2012005545 A2 WO 2012005545A2 KR 2011005026 W KR2011005026 W KR 2011005026W WO 2012005545 A2 WO2012005545 A2 WO 2012005545A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- lithium
- brine
- magnesium
- boron
- calcium
- Prior art date
Links
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 123
- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 123
- 238000000034 method Methods 0.000 title claims abstract description 35
- 238000000605 extraction Methods 0.000 title claims abstract description 22
- 229910001386 lithium phosphate Inorganic materials 0.000 claims abstract description 48
- TWQULNDIKKJZPH-UHFFFAOYSA-K trilithium;phosphate Chemical compound [Li+].[Li+].[Li+].[O-]P([O-])([O-])=O TWQULNDIKKJZPH-UHFFFAOYSA-K 0.000 claims abstract description 48
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000000463 material Substances 0.000 claims abstract description 24
- 239000012267 brine Substances 0.000 claims description 120
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 120
- 229910052796 boron Inorganic materials 0.000 claims description 95
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 93
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 claims description 81
- 239000011777 magnesium Substances 0.000 claims description 75
- 229910052749 magnesium Inorganic materials 0.000 claims description 75
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 74
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 59
- 239000000347 magnesium hydroxide Substances 0.000 claims description 59
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 59
- 239000000243 solution Substances 0.000 claims description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 39
- 239000000706 filtrate Substances 0.000 claims description 38
- 239000011575 calcium Substances 0.000 claims description 35
- 229910052791 calcium Inorganic materials 0.000 claims description 35
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 34
- 230000001376 precipitating effect Effects 0.000 claims description 28
- 239000012535 impurity Substances 0.000 claims description 20
- 239000000203 mixture Substances 0.000 claims description 16
- 238000001914 filtration Methods 0.000 claims description 12
- 229910019142 PO4 Inorganic materials 0.000 claims description 11
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 10
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 10
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 10
- 239000000920 calcium hydroxide Substances 0.000 claims description 10
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 10
- 239000010452 phosphate Substances 0.000 claims description 9
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 9
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 8
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 5
- 150000002500 ions Chemical class 0.000 claims description 4
- 239000000843 powder Substances 0.000 claims description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 30
- 229960005069 calcium Drugs 0.000 description 26
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 description 20
- 229910052808 lithium carbonate Inorganic materials 0.000 description 19
- -1 boron ions Chemical class 0.000 description 16
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 12
- 229910001416 lithium ion Inorganic materials 0.000 description 12
- LWIHDJKSTIGBAC-UHFFFAOYSA-K tripotassium phosphate Chemical compound [K+].[K+].[K+].[O-]P([O-])([O-])=O LWIHDJKSTIGBAC-UHFFFAOYSA-K 0.000 description 10
- 239000001488 sodium phosphate Substances 0.000 description 9
- 239000002244 precipitate Substances 0.000 description 7
- RYFMWSXOAZQYPI-UHFFFAOYSA-K trisodium phosphate Chemical compound [Na+].[Na+].[Na+].[O-]P([O-])([O-])=O RYFMWSXOAZQYPI-UHFFFAOYSA-K 0.000 description 7
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 6
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 239000003513 alkali Substances 0.000 description 6
- 229910001424 calcium ion Inorganic materials 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 230000008020 evaporation Effects 0.000 description 6
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 5
- 238000002835 absorbance Methods 0.000 description 5
- 238000001354 calcination Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 229910001425 magnesium ion Inorganic materials 0.000 description 5
- 230000035484 reaction time Effects 0.000 description 5
- 239000013535 sea water Substances 0.000 description 5
- 229910000162 sodium phosphate Inorganic materials 0.000 description 5
- 235000011008 sodium phosphates Nutrition 0.000 description 5
- 125000000008 (C1-C10) alkyl group Chemical group 0.000 description 4
- 239000004254 Ammonium phosphate Substances 0.000 description 4
- 229910000148 ammonium phosphate Inorganic materials 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000001506 calcium phosphate Substances 0.000 description 4
- 230000003247 decreasing effect Effects 0.000 description 4
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 3
- UFHFLCQGNIYNRP-VVKOMZTBSA-N Dideuterium Chemical compound [2H][2H] UFHFLCQGNIYNRP-VVKOMZTBSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 239000000284 extract Substances 0.000 description 3
- 150000002431 hydrogen Chemical group 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 229940083608 sodium hydroxide Drugs 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical compound O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 description 2
- 235000019289 ammonium phosphates Nutrition 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- YYRMJZQKEFZXMX-UHFFFAOYSA-L calcium bis(dihydrogenphosphate) Chemical compound [Ca+2].OP(O)([O-])=O.OP(O)([O-])=O YYRMJZQKEFZXMX-UHFFFAOYSA-L 0.000 description 2
- 238000000975 co-precipitation Methods 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- NEFBYIFKOOEVPA-UHFFFAOYSA-K dicalcium phosphate Chemical compound [Ca+2].[Ca+2].[O-]P([O-])([O-])=O NEFBYIFKOOEVPA-UHFFFAOYSA-K 0.000 description 2
- ZPWVASYFFYYZEW-UHFFFAOYSA-L dipotassium hydrogen phosphate Chemical compound [K+].[K+].OP([O-])([O-])=O ZPWVASYFFYYZEW-UHFFFAOYSA-L 0.000 description 2
- BNIILDVGGAEEIG-UHFFFAOYSA-L disodium hydrogen phosphate Chemical compound [Na+].[Na+].OP([O-])([O-])=O BNIILDVGGAEEIG-UHFFFAOYSA-L 0.000 description 2
- 230000003028 elevating effect Effects 0.000 description 2
- 150000004679 hydroxides Chemical class 0.000 description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 235000010755 mineral Nutrition 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 235000019691 monocalcium phosphate Nutrition 0.000 description 2
- 229910000150 monocalcium phosphate Inorganic materials 0.000 description 2
- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 2
- 235000019796 monopotassium phosphate Nutrition 0.000 description 2
- 229910000403 monosodium phosphate Inorganic materials 0.000 description 2
- 235000019799 monosodium phosphate Nutrition 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- GNSKLFRGEWLPPA-UHFFFAOYSA-M potassium dihydrogen phosphate Chemical compound [K+].OP(O)([O-])=O GNSKLFRGEWLPPA-UHFFFAOYSA-M 0.000 description 2
- 229910000160 potassium phosphate Inorganic materials 0.000 description 2
- 235000011009 potassium phosphates Nutrition 0.000 description 2
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 description 2
- GCLGEJMYGQKIIW-UHFFFAOYSA-H sodium hexametaphosphate Chemical compound [Na]OP1(=O)OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])O1 GCLGEJMYGQKIIW-UHFFFAOYSA-H 0.000 description 2
- 235000019982 sodium hexametaphosphate Nutrition 0.000 description 2
- 239000001577 tetrasodium phosphonato phosphate Substances 0.000 description 2
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 2
- 229910000391 tricalcium phosphate Inorganic materials 0.000 description 2
- 235000019731 tricalcium phosphate Nutrition 0.000 description 2
- 229940078499 tricalcium phosphate Drugs 0.000 description 2
- 229910000404 tripotassium phosphate Inorganic materials 0.000 description 2
- 235000019798 tripotassium phosphate Nutrition 0.000 description 2
- 229910000406 trisodium phosphate Inorganic materials 0.000 description 2
- 235000019801 trisodium phosphate Nutrition 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- LRXTYHSAJDENHV-UHFFFAOYSA-H zinc phosphate Chemical compound [Zn+2].[Zn+2].[Zn+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O LRXTYHSAJDENHV-UHFFFAOYSA-H 0.000 description 2
- 229910000165 zinc phosphate Inorganic materials 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 229910006130 SO4 Inorganic materials 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- HEHRHMRHPUNLIR-UHFFFAOYSA-N aluminum;hydroxy-[hydroxy(oxo)silyl]oxy-oxosilane;lithium Chemical compound [Li].[Al].O[Si](=O)O[Si](O)=O.O[Si](=O)O[Si](O)=O HEHRHMRHPUNLIR-UHFFFAOYSA-N 0.000 description 1
- CNLWCVNCHLKFHK-UHFFFAOYSA-N aluminum;lithium;dioxido(oxo)silane Chemical compound [Li+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O CNLWCVNCHLKFHK-UHFFFAOYSA-N 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- 239000003637 basic solution Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- PEYVWSJAZONVQK-UHFFFAOYSA-N hydroperoxy(oxo)borane Chemical compound OOB=O PEYVWSJAZONVQK-UHFFFAOYSA-N 0.000 description 1
- 229910052629 lepidolite Inorganic materials 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910052670 petalite Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 125000001436 propyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 229910052642 spodumene Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
- C22B26/10—Obtaining alkali metals
- C22B26/12—Obtaining lithium
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/30—Alkali metal phosphates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/30—Alkali metal phosphates
- C01B25/301—Preparation from liquid orthophosphoric acid or from an acid solution or suspension of orthophosphates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/30—Alkali metal phosphates
- C01B25/308—Methods for converting an alkali metal orthophosphate into another one; Purification; Decolorasing; Dehydrating; Drying
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
- C22B26/20—Obtaining alkaline earth metals or magnesium
- C22B26/22—Obtaining magnesium
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Definitions
- the present invention relates to a method of extracting lithium from a lithium bearing solution.
- the application of lithium currently extends to diverse industries,including the rechargeable battery, glass, ceramic, alloy, lubricant, and pharmaceutical industries.
- the lithium rechargeable battery has recently been receiving attention as a main power source for hybrid and electric cars, and the market for lithium rechargeable batteries for cars is expected to continue growing to approximately one-hundred times the conventional compact battery markets for cell phones and notebooks.
- the main sources for the lithium could be minerals, brine and seawater. Although minerals such as spodumene, petalite and lepidolite contain relatively large amountsof lithium, ranging from approximately 1 to 1.5%, the extraction involves complicated processes such as floatation, calcining at a high temperature, grinding, acid mixing, extraction, purification, concentration and precipitation. These processes, require high energy consumption, are considered to be cost-ineffective, and the use of acids during the lithium extraction also causes environmental pollution.
- lithium is currently extracted from brine produced from natural salt lakes, but salts such as Mg, Ca, B, Na, K, SO 4 are also dissolved in the brine.
- the concentration of lithium contained in the brine ranges from approximately 0.3 to 1.5g/L, and lithium contained in the brine is usually extracted in the form of lithium carbonate having a solubility of about 13g/L. Even assumingthat lithium contained in the brine is completely converted to lithium carbonate, the concentration of lithium carbonate in the brine is limited to 1.59 to 7.95g/L (the molecular weight of Li 2 CO 3 is 74, and the atomic weight of Li is 7. If the concentration of lithium is multiplied by 5.3 (74 ⁇ 14 ⁇ .3), the concentration of lithium carbonate can be estimated). Since most of the lithium carbonate concentration is lower than the solubility of lithium carbonate, the extracted lithium carbonate re-dissolves,and thus there is a problem of the lithium extraction yield being extremely low.
- the brine pumped from the natural salt lake was stored in evaporation ponds and subsequently naturally evaporated outdoors over a long period of time, for instance about one year, to concentrate the lithium by several tenfold. Then, the impurities such as magnesium, calcium, boron were precipitated in order to be removed, and the method required an amount greater than the solubility of lithium carbonate to precipitate.
- Chinese Patent Pub. No. 1,626,443 describes a method of extracting lithium, wherein brine is evaporated and concentrated under solar heat, and the concentrate is subject to repeated electro-dialysis in order to obtain brine containing concentrated lithium with a low amount of magnesium.
- a method of economical extraction of high purity lithium phosphate with high extraction yield from brine which does not require the processes of evaporation and concentration of the brine for a long period of time, by using lithium phosphate having low solubility may be provided.
- a method of economical extraction of lithium from a lithium bearing solution by adding a phosphorous supplying material to the solution to precipitate lithium phosphate from the dissolved lithium is provided.
- the phosphorous supplying material may be one selected from the group consisting of phosphorous, phosphoric acid, phosphate and a mixture thereof.
- the concentration of the lithium phosphate may be 0.39g/L or more.
- the concentration of lithium in the lithium bearing solution may be 0.1g/L or more. More specifically, the concentration may be 0.2g/L or more, or 0.5g/L or more. The concentration of 60g/L or more, however, may not be economical because a great amount of time is required for the high-enrichment of lithium.
- the method may further comprise a step of extracting lithium phosphate by filtering the precipitated lithium phosphate from the lithium bearing solution.
- the lithium bearing solution may be brine.
- the brine may contain impurities including magnesium, boron, calcium, or a mixture thereof.
- the method may further comprise a step of precipitating and removing impurities in the brine, including magnesium, boron, calcium, or a mixture thereof by adding a hydroxyl ion in the brine.
- the step ofprecipitating lithium phosphate from dissolved lithium by adding a phosphorous supplying material may be performed at room temperature or higher.
- the hydroxyl ion may be a negative ion of sodium hydroxide.
- the step of precipitating and removing impurities in the brine, including magnesium, boron, calcium, or a mixture thereof by adding a hydroxyl ion in the brine may be a step of precipitating and removing impurities in the brine, including magnesium, boron and calcium, by adding a hydroxyl ion in the brine.
- the step of precipitating and removing impurities in the brine, including magnesium, boron and calcium, by adding a hydroxyl ion in the brine may further comprise the steps of:(a) producing magnesium hydroxide from the magnesium by adding a hydroxyl ion in the brine; (b) absorbing boron inthe magnesium hydroxide to extract magnesium and boron by co-precipitating magnesium and boron; and (c) precipitating calcium by adjusting the pH of the filtrate from which magnesium and boron are removed to be at least 12.
- the step of producing magnesium hydroxide from the magnesium by adding a hydroxyl ion in the brine may be a step of producing magnesium hydroxide from the magnesium by adding a hydroxyl ion while maintaining the pH of the brine to be in the range of 8.5 to 10.5.
- the step of absorbing boron in the magnesium hydroxide to extract magnesium and boron by co-precipitatingmagnesium and boron may be performed by absorbing the boron in the brine including the magnesium hydroxide having a pH ranging from 8.5 to 10.5 inthe magnesium hydroxide to extract magnesium and boron by co-precipitating magnesium and boron.
- the step of producing magnesium hydroxide from the magnesium by adding a hydroxyl ion in the brine, while maintaining the pH of the brine to be in the range of 8.5 to 10.5 by adding a hydroxyl ion in the brine, and the step of absorbing the boron in the brine including the magnesium hydroxide having apH ranging from 8.5 to 10.5 in the magnesium hydroxide to extract magnesium and boron by co-precipitatingmagnesium and boron may be performed simultaneously.
- the step of precipitating lithium phosphate from dissolved lithium by adding a phosphorous supplying material may be followed by a step of filtering the precipitated lithium phosphate and extracting it in the form of a high purity powder.
- thestep of precipitating calcium by adjusting the pH of the filtrate from which magnesium and boron are removed to be at least 12 may be a step of precipitating calcium hydroxide or calcium carbonate from calcium by adding hydroxyl ion, carbonate ion, or a mixture thereof.
- lithium dissolved in the brine may be economically extracted as lithium with high extraction yield by precipitation using lithium phosphate having low solubility.
- FIG. 1 is a graph depicting the surface charge change of magnesium hydroxide according to the pH of the brine.
- FIG. 2 is a graph depicting the concentration change of magnesium ions in the filtrate relative to the NaOH addition amount.
- FIG. 3 is a graph depicting the concentration change of boron ions in the filtrate relative to the NaOH addition amount.
- FIG. 4 is a graph depicting the concentration change of lithium ions in the filtrate relative to the NaOH addition amount.
- FIG. 5 is a graph depicting the concentration change of calcium ions in the filtrate relative to the NaOH addition amount.
- FIG. 6 is a graph depicting the concentration of lithium relative to the reaction time when lithium phosphate is precipitated from lithium.
- FIG. 7 is a graph depicting the concentration of lithium relative to the reaction time and temperature when lithium phosphate is precipitated from lithium.
- FIG. 8 is a graph depicting the concentration of lithium phosphate in the filtrate relative to the reaction time when lithium carbonate is precipitated from lithium.
- a method of economical and efficient extraction of lithium from a lithium bearing solution by adding a phosphorous supplying material to the solution to precipitate lithium phosphate instead of lithium carbonate from the dissolved lithium may be provided.
- lithium carbonate Li 2 CO 3
- the solubility of lithium phosphate (Li 3 PO 4 ), however, is approximately 0.39g/L, which is relatively lower than that of lithium carbonate. Accordingly, it is possible to extract even a small concentration of 0.5g/L or1.5g/L of lithium dissolved in the lithium bearing solution, such as brine, which can be precipitated and separated into lithium phosphate in a solid state by adding a phosphorous supplying material in the lithium bearing solution.
- the concentration of lithium in the lithium bearing solution may be 0.1g/L or more. More specifically, the concentration may be 0.2g/L or more, or 0.5g/L or more. The concentration of 60g/L or more, however, may not be economical because a great amount of time is required for the high-enrichment of lithium.
- the phosphorous supplying material selected from the group consisting of phosphorous, phosphoric acid, phosphate, and a mixture thereof is added to the lithium bearing solution to produce lithium phosphate.
- the concentration i.e., the dissolved concentration in the lithium bearing solution
- the concentration should be 0.39g/L or greater.
- the phosphorous supplying material is a compound capable of altering the pH of the lithium bearing solution (e.g., phosphoric acid)
- hydroxide ions can be concurrently used to prevent the precipitated lithium phosphate from re-dissolving once the pH of the solution decreases.
- the phosphate may be, for example, but is not limited thereto, potassium phosphate, sodium phosphate, and ammonium phosphate.
- the ammonium may be (NR 4 ) 3 PO 4 , wherein R is independently a hydrogen, a heavy hydrogen, a substituted or unsubstituted C1-C10 alkyl group, but not limited thereto.
- the phosphate may be, for example, but is not limited thereto, mono-potassium phosphate, di-potassium phosphate, tri-potassium phosphate, mono-sodium phosphate, di-sodium phosphate, tri-sodium phosphate, aluminum phosphate, zinc phosphate, poly-ammonium phosphate, sodium-hexa-meta-phosphate, mono-calcium phosphate, di-calcium phosphate, and tri-calcium-phosphate.
- the phosphorous supplying material may be water-soluble. In the case the phosphorous supplying material is water-soluble, the reaction with lithium contained in the lithium bearing solution may easily occur.
- the precipitated lithium phosphate may be extracted by filtering the lithium bearing solution.
- the method of economical extraction of lithium from a lithium bearing solution by adding a phosphorous supplying material to the solution to precipitate lithium phosphate from the dissolved lithium may be performed at room temperature. More specifically, the temperature may be more than 20°C, 30°C, 50°Cor 90°C.
- room temperature is not limited to a definite temperature, and it is construed to mean a temperature without the application of external energy. Accordingly, the room temperature may vary depending on time and place.
- a step of removing impurities in the brine, including magnesium, boron or calcium, by adding a hydroxyl ion in a lithium bearing solution (e.g., brine) followed by precipitating may be included.
- the hydroxyl ion may be, for example, but is not limited thereto, sodium hydroxide, potassium hydroxide, ammonium hydroxide.
- the ammonium may be (NR 4 ) 3 OH, wherein R is independently a hydrogen, a heavy hydrogen, a substituted or unsubstituted C1-C10 alkyl group, but is not limited thereto.
- the hydroxide may be an anion of sodiumhydroxide.
- the hydroxyl ion may be an anion of hydroxide salt produced as a by-product during the extraction of lithium, because the cation of hydroxide salt has high solubility.
- the step of precipitating and removing impurities in the brine, including magnesium, boron or calcium, by adding a hydroxyl ion in the lithium bearing solution may be a step of precipitating and removing impurities in the brine, including magnesium, boron and calcium, by adding a hydroxyl ion in the brine.
- the step of precipitating and removing impurities in the brine, including magnesium, boron or calcium, by adding a hydroxyl ionin the brine may further comprise the steps of: (a) producing magnesium hydroxide from the magnesium by adding a hydroxyl ion in the brine; (b) absorbing boron in the magnesium hydroxide to extract magnesium and boron by co-precipitatingmagnesium and boron; and (c) precipitating calcium by adjusting the pH of the filtrate from which magnesium and boron are removed to be at least 12.
- the step of (a) producing magnesium hydroxide from the magnesium by adding a hydroxyl ion in the brine and the step of (b) absorbing boron in the magnesium hydroxide to extract magnesium and boron by co-precipitating magnesium and boron may be performed individually or concurrently.
- steps (a) and (b) may be performed simultaneously, whereas the steps may be performed separately if the amount of magnesium produced is insufficient.
- the magnesium may be produced as magnesium hydroxide by adding a hydroxyl ion (e.g.,NaOH) to a lithium bearing brine including magnesium, boron, and calcium.
- a hydroxyl ion e.g.,NaOH
- a lithium bearing brine including magnesium, boron, and calcium.
- the pH of the brine with the added hydroxyl ion (e.g., NaOH) may be adjusted to be between 8.5 and 10.5 and subsequently, the co-precipitation of magnesium and boron may be possible by absorbing boron in the magnesium hydroxide.
- the steps may be performed concurrently.
- magnesium dissolved in the brine may be precipitated as magnesium hydroxide by adding a hydroxyl ion (e.g., NaOH).
- a hydroxyl ion e.g., NaOH
- Magnesium hydroxide is characterized in having a low solubility of 0.009g/L, and has a tendency to easily precipitate in a basic solution having a pH of 8 or higher.
- boron e.g., boron ions
- boron ions may be absorbed on the surface of the produced magnesium hydroxide to co-precipitate magnesium and boron.
- the surface charge of the magnesium hydroxide can be utilized.
- the surface charge of the magnesium hydroxide is greatly influenced by the pH of the solution.
- the boron ions existing in the form of a negative ion such as H 2 BO 3 - or HBO 3 2-
- the surface charge of the magnesium hydroxide is negative, however, the negatively charged boron ions arenot absorbed in the magnesium hydroxide.
- a hydroxyl ion e.g., NaOH
- a hydroxyl ion e.g., NaOH
- a hydroxyl ion e.g.,NaOH
- boron e.g.,boron ions
- an additional hydroxyl ion e.g., NaOH
- an additional hydroxyl ion may be added to the filtrate to adjust the pH to be between 8.5 and 10.5 and subsequently precipitate the remaining magnesium and boron.
- hydroxyl ion e.g., NaOH
- the pH of the brine is not likely to be maintained at between 8.5 and 10.5, and thus the co-precipitation efficiency of magnesium and boron is likely to drop as well, resulting in the loss of lithium.
- Calcium may be precipitated by adding a hydroxyl ion or carbonate ion (e.g., NaOH, carbonate, or a mixture thereof) to the filtrate from which magnesium and boron are extracted to adjust the pH to be 12 or higher.
- a hydroxyl ion or carbonate ion e.g., NaOH, carbonate, or a mixture thereof
- calcium hydroxide or carbonate hydroxide may be precipitated.
- the filtration step to separate the precipitated magnesium hydroxide absorbed with the boron from the brine is omitted, and the pH is adjusted to be 12 or higher to eliminate calcium, the surface charge of magnesium hydroxide would be converted to negative,because the pH of the brine deviates from the range of 8.5 and 10.5.
- the boron absorbed inthe magnesium hydroxide will be desorbed, and instead, positive lithium ions will be absorbed, causing both the loss of lithium and a decrease in the boron extraction yield.
- the calcium hydroxide and the calcium carbonate having very lowsolubility, are easily precipitated when the pH is 12 or higher. Thus, it is preferable to maintain the pH of the filtrate to be 12 or higher.
- a mixture of an alkali and carbonate can be added.
- the alkali is selected from the group consisting of NaOH, KOH, Ca(OH) 2 , NH 4 OH, R 4 NOH ⁇ 5H 2 0 and a mixture thereof, wherein R is independently a C1-C10 alkyl group, such as, methyl, ethyl, propyl or butyl.
- alkali e.g., NaOH
- a significant amount of alkali e.g., NaOH
- the pH could be economically maintained to be at least 12 even if the amount of alkali could be relatively reduced.
- the carbonate is selected from the group having high solubility consisting of Na 2 CO 3 , K 2 CO 3 , and a mixture thereof, and sodium and potassium included in the carbonate are dissolved in the filtrate.
- the precipitated calcium hydroxide or calcium carbonate is separated from the remaining filtrate, and subsequently calcium is extracted.
- a phosphate supplying material may be added to the remaining filtrate from which the impurities are removed to precipitate lithium phosphate from lithium contained in the brine.
- the step of precipitating lithium phosphate from the lithium bearing brine may be performed at room temperature or above, or at 40°Cor above. More specifically, the step may be performed at 50°Cor above, 60°Cor above, 70°Cor above, 80°Cor above, or 90°Cor above.
- the phosphorous supplying material may be selected from the group consisting of phosphorous, phosphoric acid, phosphate, and a mixture thereof.
- the concentration i.e., the dissolved concentration in the lithium bearing solution
- the concentration should be 0.39g/L or greater.
- the phosphate may be, for example, but is not limited thereto, potassium phosphate, sodium phosphate, and ammonium phosphate.
- the ammonium may be (NR 4 ) 3 PO 4 , wherein R is independently a hydrogen, a heavy hydrogen, a substituted or unsubstituted C1-C10 alkyl group, but not limited thereto.
- the phosphate may be, for example, but is not limited thereto, mono-potassium phosphate, di-potassium phosphate, tri-potassium phosphate, mono-sodium phosphate, di-sodium phosphate, tri-sodium phosphate, aluminum phosphate, zinc phosphate, poly-ammonium phosphate, sodium-hexa-meta-phosphate, mono-calcium phosphate, di-calcium phosphate, and tri-calcium-phosphate.
- the phosphorous supplying material may be water-soluble. In the case the phosphorous supplying material is water-soluble, the reaction with lithium contained in the lithium bearing solution may easily occur.
- the filtrate is calcinatedfor 10 to 15 minutes at room temperature, or at a temperature range of 40-200°C, 50-200°C, 60-200°C, 70-200°C, 80-200°C, or 90-200°C.
- the step of extracting the precipitated lithium phosphate filtered from the filtrate may be performed.
- the extracted lithium phosphate may be washed to obtain high purity lithium phosphate powder.
- NaOH was added to brine containing magnesium ions 20,000ppm, boron ions 900ppm, calcium ions350ppm, and lithium ions 900ppm to precipitate magnesium hydroxide. While adjusting the pH of the brine, the surface charge of the precipitated magnesium hydroxide was measured. The results are shown in FIG. 1.
- the surface charge of the magnesium hydroxide was maintained with a positive charge when the pH range of the NaOH added brine was between 8.5 and 10.5. Accordingly, the boron ionswith a negative charge were easily absorbed on the magnesium hyrdroxide, and the positively charged lithium ions were prevented from being absorbed. This minimized the loss of lithium, and efficiently extracted both magnesium and boron from the brine at the same time.
- magnesium hydroxide was precipitated from the brine containing magnesium ions20,000ppm, boron ions 900ppm, calcium ions 350ppm, and lithium ions900ppm. Subsequently, a filtration was performed to separate the precipitated magnesium hydroxide from the brine. The filtrate was collected to measure the amount of magnesium, boron and lithium. The results are shown in FIGs.2, 3, and 4, respectively.
- the amount of boron ions dissolved in the brine initially decreased as the amount of NaOH added increased. This may be explained by the fact that the pH change could be insignificantly affected by the addition of NaOH in the beginning, and the surface charge of the magnesium hydroxide precipitated from the brine having a pH value of 10.5 or lower had a positive charge. Thus, the negatively charged boron ions present in the filtrate were precipitated while adsorbed on the surface of the magnesium hydroxide.
- the amount of lithum ions present in the filtrate were initially not influenced by the addedamount of NaOH. This could be explained by the fact that the positively charged lithium ionsexisting in the lithium bearing solution were not absorbed inthe magnesium hydroxide because the surface charge of magnesium hydroxide had a positive charge in the beginning. If an excessive amount of NaOH was added, however, the pH of the brine surpassed 10.5. Then, the surface charge of the magnesium hydroxide was converted to a negative charge and the negatively charged boron ions werenot absorbed to the surface. Consequently, the concentration of boron ionsexisting in the filtrate dramatically increased. On the contrary, the concentration of positively charged lithium ions existing in the filtrate rapidly decreased as the lithium ions were absorbed to the surface of the magnesium hydroxide.
- NaOH wasadded to the brine containing magnesium ions 20,000ppm, boron ions900ppm, calcium ions 350ppm, and lithium ions 900ppm to precipitate calcium hydroxide from the solution containing calcium ions. Subsequently, a filtration was performed to separate the precipitated calcium hydroxide from the brine. The resulting filtrate was collectedto measure the amount of calcium. The result is shown in FIG. 5.
- the pH of the lithium bearing solution is at least 12 in order to enhance the extract yield of the calcium ions from the brine.
- the pH of the brine was prematurely adjusted to be at least 12 in the beginning, the surface charge of the precipitated magnesium hydroxide had a negative charge. This preventedthe absorbance of the boron ions and caused the loss of lithium due to the absorbance of positively charged lithium ions.
- the pH of the brine Prior to extracting calcium by adding NaOH, the pH of the brine was adjusted to be between 8.5 and 10.5 so that the magnesium hydroxide having a positive charge was precipitated to prevent the absorbance of the lithium ions. Once the boron ions were absorbed, the simultaneous extraction of magnesium and boron was performed. Then, the pH of the remaining filtrate from which magnesium and boron were extracted wasadjusted to be at least 12 to precipitate the calcium hydroxide from calcium.
- the impurities including magnesium, calcium and boron, were removed from the brine, and 7.217g/L of sodium phosphate was added to the remaining filtrate dissolved with the concentration of lithium ions being 0.917g/L.
- the filtrate was maintained to be reacted for 15 to 60 minutes, while elevating the temperature to 90°C.
- the concentration of lithium in the filtrate initially decreased dramatically when sodium phosphate was added to the brine. After the reaction time passed 15 minutes, the concentration of lithium in the filtrate came to be below 50 mg/L. This indicated that more than 95% of lithium dissolved in the brine was precipitated and separated as lithium phosphate.
- lithium phosphate Since the solubility of lithium phosphate is approximately 0.39g/L, which is much lower than the solubility of lithium carbonate, adding a material including phosphorous, such as sodium phosphate, in the brine precipitated lithium phosphate in the form of solid from a small amount of lithium dissolved in the brine.
- a material including phosphorous such as sodium phosphate
- the lithium extraction yield was more than 90% after the reaction time of 10 minutes, and the yield was more than 95% after 15 minutes.
- the impurities including magnesium, calcium and boron, were removed from the brine, and 7g/L of sodium carbonatewas added to the remaining filtrate dissolved with the concentration of lithium ions being 0.917g/L.
- the filtrate was maintained to be reacted for 15 to 60 minutes, while elevating the temperature to 90°C
- lithium phosphate having a low solubility By precipitating lithium dissolved in the brine by using lithium phosphate having a low solubility, the processes of evaporation as well as concentration of brine are not required, and the economical extraction of lithium with high extraction yield, while minimizing the loss of lithium, may be possible.
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Manufacturing & Machinery (AREA)
- Environmental & Geological Engineering (AREA)
- Metallurgy (AREA)
- Life Sciences & Earth Sciences (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Extraction Or Liquid Replacement (AREA)
- Removal Of Specific Substances (AREA)
Abstract
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2013519573A JP5587500B2 (ja) | 2010-07-09 | 2011-07-08 | リチウム含有溶液からリチウムを抽出する方法 |
EP11803831.4A EP2591130B1 (fr) | 2010-07-09 | 2011-07-08 | Procédé pour l'extraction économique de lithium à partir d'une solution comprenant du lithium |
CN2011800394188A CN103069022A (zh) | 2010-07-09 | 2011-07-08 | 从含锂溶液中经济地提取锂的方法 |
US13/736,143 US8778289B2 (en) | 2010-07-09 | 2013-01-08 | Method for economical extraction of lithium from solution including lithium |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR20100066391 | 2010-07-09 | ||
KR10-2010-0066391 | 2010-07-09 | ||
KR10-2010-0124089 | 2010-12-07 | ||
KR20100124089 | 2010-12-07 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US13/736,143 Continuation US8778289B2 (en) | 2010-07-09 | 2013-01-08 | Method for economical extraction of lithium from solution including lithium |
Publications (3)
Publication Number | Publication Date |
---|---|
WO2012005545A2 true WO2012005545A2 (fr) | 2012-01-12 |
WO2012005545A3 WO2012005545A3 (fr) | 2012-04-26 |
WO2012005545A4 WO2012005545A4 (fr) | 2012-06-14 |
Family
ID=45441678
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/KR2011/005026 WO2012005545A2 (fr) | 2010-07-09 | 2011-07-08 | Procédé pour l'extraction économique de lithium à partir d'une solution comprenant du lithium |
Country Status (8)
Country | Link |
---|---|
US (1) | US8778289B2 (fr) |
EP (1) | EP2591130B1 (fr) |
JP (1) | JP5587500B2 (fr) |
CN (2) | CN103069022A (fr) |
AR (1) | AR082147A1 (fr) |
CL (1) | CL2013000061A1 (fr) |
PT (1) | PT2591130T (fr) |
WO (1) | WO2012005545A2 (fr) |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102815680A (zh) * | 2012-08-14 | 2012-12-12 | 焦作氟多凯工业有限公司 | 一种利用含锂废液生产磷酸锂的方法 |
JP2015515440A (ja) * | 2012-04-05 | 2015-05-28 | ポスコ | 水酸化リチウムの製造方法およびこれを用いた炭酸リチウムの製造方法 |
CN104884648A (zh) * | 2012-12-21 | 2015-09-02 | 浦项产业科学研究院 | 从含锂溶液中提取锂的方法 |
US9994931B2 (en) | 2012-07-31 | 2018-06-12 | Posco | Method for extracting lithium from solution containing lithium |
US11253848B2 (en) | 2017-08-02 | 2022-02-22 | Lilac Solutions, Inc. | Lithium extraction with porous ion exchange beads |
US11339457B2 (en) * | 2020-01-09 | 2022-05-24 | Lilac Solutions, Inc. | Process for separating undesirable metals |
US11358875B2 (en) | 2020-06-09 | 2022-06-14 | Lilac Solutions, Inc. | Lithium extraction in the presence of scalants |
US11377362B2 (en) | 2020-11-20 | 2022-07-05 | Lilac Solutions, Inc. | Lithium production with volatile acid |
US11806641B2 (en) | 2016-11-14 | 2023-11-07 | Lilac Solutions, Inc. | Lithium extraction with coated ion exchange particles |
US11865531B2 (en) | 2018-02-28 | 2024-01-09 | Lilac Solutions, Inc. | Ion exchange reactor with particle traps for lithium extraction |
US11986816B2 (en) | 2021-04-23 | 2024-05-21 | Lilac Solutions, Inc. | Ion exchange devices for lithium extraction |
Families Citing this family (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2603620A4 (fr) * | 2010-08-12 | 2016-10-12 | Res Inst Ind Science & Tech | Procédé pour extraire du lithium haute pureté d'une solution comprenant du lithium par électrolyse |
KR101659799B1 (ko) * | 2014-12-19 | 2016-09-27 | 재단법인 포항산업과학연구원 | 금속리튬의 제조 방법 |
KR101604954B1 (ko) * | 2015-09-22 | 2016-03-18 | 강원대학교산학협력단 | 폐전지의 리튬폐액을 활용한 고순도 인산리튬 제조방법 |
CN109312483B (zh) * | 2016-06-07 | 2021-06-22 | 浦项产业科学研究院 | 金属锂的制备方法 |
CA3071649A1 (fr) | 2017-08-02 | 2019-02-07 | Lilac Solutions, Inc. | Systeme d'echange d'ions pour extraction de lithium |
CN111527046A (zh) * | 2017-12-22 | 2020-08-11 | 株式会社Posco | 磷酸锂的制备方法、氢氧化锂的制备方法及碳酸锂的制备方法 |
US10648090B2 (en) | 2018-02-17 | 2020-05-12 | Lilac Solutions, Inc. | Integrated system for lithium extraction and conversion |
CN108193054B (zh) * | 2018-03-12 | 2020-01-14 | 中国科学院过程工程研究所 | 一种从含锂废水中提取锂的方法 |
CN108423696A (zh) * | 2018-04-18 | 2018-08-21 | 中国科学院过程工程研究所 | 从含锂溶液中提取高纯锂盐的方法 |
US20210206651A1 (en) * | 2018-05-30 | 2021-07-08 | Lithium Australia Nl | Process for recovering lithium values |
KR102070435B1 (ko) * | 2018-07-04 | 2020-01-28 | 전웅 | 리튬 추출 방법 |
WO2021145488A1 (fr) * | 2020-01-17 | 2021-07-22 | 전웅 | Procédé d'extraction de lithium |
JP2023529256A (ja) * | 2021-05-07 | 2023-07-10 | ヨン・ブン・コーポレーション | 乾式溶融方法を利用した廃リチウム二次電池からリチウムを回収する方法 |
CN113415791B (zh) * | 2021-06-25 | 2022-11-29 | 云南云天化红磷化工有限公司 | 湿法磷酸萃取生产磷酸二氢钾中萃取剂回收装置及其方法 |
CN114132907A (zh) * | 2021-11-05 | 2022-03-04 | 安徽大学绿色产业创新研究院 | 一种从高纯碳酸锂的沉锂母液中回收锂的方法 |
CN114797768B (zh) * | 2022-03-22 | 2023-08-11 | 中南大学 | 一种磷酸镁复盐-活性炭复合材料及其制备方法和作为钾离子吸附材料的应用 |
US11873228B2 (en) | 2022-04-08 | 2024-01-16 | Uong CHON | Method of extracting lithium, method of preparing lithium carbonate and method of preparing lithium hydroxide |
CN115536047A (zh) * | 2022-11-11 | 2022-12-30 | 神华准能资源综合开发有限公司 | 利用含锂废水制备碳酸锂的方法 |
Family Cites Families (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP4217292B2 (ja) * | 1998-03-17 | 2009-01-28 | 株式会社東芝 | リチウム回収方法 |
US7157065B2 (en) * | 1998-07-16 | 2007-01-02 | Chemetall Foote Corporation | Production of lithium compounds directly from lithium containing brines |
US6921522B2 (en) * | 1998-07-16 | 2005-07-26 | Chemetall Foote Corporation | Production of lithium compounds directly from lithium containing brines |
US6207126B1 (en) * | 1998-07-16 | 2001-03-27 | Chemetall Foote Corporation | Recovery of lithium compounds from brines |
US6528033B1 (en) * | 2000-01-18 | 2003-03-04 | Valence Technology, Inc. | Method of making lithium-containing materials |
JP4620378B2 (ja) * | 2003-05-09 | 2011-01-26 | 日本化学工業株式会社 | リン酸リチウム凝集体、その製造方法及びリチウム鉄リン系複合酸化物の製造方法 |
JP4581553B2 (ja) * | 2004-08-20 | 2010-11-17 | 住友金属鉱山株式会社 | リチウムの回収方法 |
JP4892925B2 (ja) * | 2005-10-25 | 2012-03-07 | 住友金属鉱山株式会社 | リチウムイオン電池からの有価金属回収方法 |
JP4767798B2 (ja) * | 2006-09-05 | 2011-09-07 | 住友大阪セメント株式会社 | 電極材料の製造方法、リチウムの回収方法、正極材料及び電極並びに電池 |
NO328264B1 (no) * | 2008-01-30 | 2010-01-18 | Elkem Solar As | Fremgangsmate for fremstilling av kalsiumforbindelser |
CA2725443C (fr) * | 2008-04-22 | 2013-07-02 | Chemetall Foote Corporation | Procede de realisation d'hydroxyde de lithium et d'acide chlorhydrique de haute purete |
US8641992B2 (en) * | 2008-07-18 | 2014-02-04 | Ady Resources Limited | Process for recovering lithium from a brine |
CN101508450B (zh) * | 2009-03-18 | 2010-12-08 | 中南大学 | 一种钙循环固相转化法从低镁锂比盐湖卤水中提取锂盐的方法 |
EP2603620A4 (fr) * | 2010-08-12 | 2016-10-12 | Res Inst Ind Science & Tech | Procédé pour extraire du lithium haute pureté d'une solution comprenant du lithium par électrolyse |
-
2011
- 2011-07-08 CN CN2011800394188A patent/CN103069022A/zh active Pending
- 2011-07-08 PT PT118038314T patent/PT2591130T/pt unknown
- 2011-07-08 CN CN201611052616.9A patent/CN107012339A/zh active Pending
- 2011-07-08 AR ARP110102467 patent/AR082147A1/es active IP Right Grant
- 2011-07-08 JP JP2013519573A patent/JP5587500B2/ja active Active
- 2011-07-08 EP EP11803831.4A patent/EP2591130B1/fr active Active
- 2011-07-08 WO PCT/KR2011/005026 patent/WO2012005545A2/fr active Application Filing
-
2013
- 2013-01-08 US US13/736,143 patent/US8778289B2/en active Active
- 2013-01-08 CL CL2013000061A patent/CL2013000061A1/es unknown
Non-Patent Citations (2)
Title |
---|
None |
See also references of EP2591130A4 |
Cited By (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2015515440A (ja) * | 2012-04-05 | 2015-05-28 | ポスコ | 水酸化リチウムの製造方法およびこれを用いた炭酸リチウムの製造方法 |
US9598291B2 (en) | 2012-04-05 | 2017-03-21 | Posco | Method for manufacturing lithium hydroxide and method using same for manufacturing lithium carbonate |
US9994931B2 (en) | 2012-07-31 | 2018-06-12 | Posco | Method for extracting lithium from solution containing lithium |
CN102815680A (zh) * | 2012-08-14 | 2012-12-12 | 焦作氟多凯工业有限公司 | 一种利用含锂废液生产磷酸锂的方法 |
CN104884648A (zh) * | 2012-12-21 | 2015-09-02 | 浦项产业科学研究院 | 从含锂溶液中提取锂的方法 |
CN104884648B (zh) * | 2012-12-21 | 2019-01-15 | 浦项产业科学研究院 | 从含锂溶液中提取锂的方法 |
US11806641B2 (en) | 2016-11-14 | 2023-11-07 | Lilac Solutions, Inc. | Lithium extraction with coated ion exchange particles |
US11794182B2 (en) | 2017-08-02 | 2023-10-24 | Lilac Solutions, Inc. | Lithium extraction with porous ion exchange beads |
US11253848B2 (en) | 2017-08-02 | 2022-02-22 | Lilac Solutions, Inc. | Lithium extraction with porous ion exchange beads |
US11865531B2 (en) | 2018-02-28 | 2024-01-09 | Lilac Solutions, Inc. | Ion exchange reactor with particle traps for lithium extraction |
US11975317B2 (en) | 2018-02-28 | 2024-05-07 | Lilac Solutions, Inc. | Ion exchange reactor with particle traps for lithium extraction |
US11339457B2 (en) * | 2020-01-09 | 2022-05-24 | Lilac Solutions, Inc. | Process for separating undesirable metals |
US11358875B2 (en) | 2020-06-09 | 2022-06-14 | Lilac Solutions, Inc. | Lithium extraction in the presence of scalants |
US11964876B2 (en) | 2020-06-09 | 2024-04-23 | Lilac Solutions, Inc. | Lithium extraction in the presence of scalants |
US11377362B2 (en) | 2020-11-20 | 2022-07-05 | Lilac Solutions, Inc. | Lithium production with volatile acid |
US11986816B2 (en) | 2021-04-23 | 2024-05-21 | Lilac Solutions, Inc. | Ion exchange devices for lithium extraction |
Also Published As
Publication number | Publication date |
---|---|
PT2591130T (pt) | 2017-08-01 |
JP5587500B2 (ja) | 2014-09-10 |
EP2591130A4 (fr) | 2015-08-19 |
WO2012005545A3 (fr) | 2012-04-26 |
CL2013000061A1 (es) | 2013-07-19 |
US8778289B2 (en) | 2014-07-15 |
CN103069022A (zh) | 2013-04-24 |
US20130129586A1 (en) | 2013-05-23 |
AR082147A1 (es) | 2012-11-14 |
WO2012005545A4 (fr) | 2012-06-14 |
JP2013535573A (ja) | 2013-09-12 |
EP2591130A2 (fr) | 2013-05-15 |
CN107012339A (zh) | 2017-08-04 |
EP2591130B1 (fr) | 2017-05-03 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2012005545A2 (fr) | Procédé pour l'extraction économique de lithium à partir d'une solution comprenant du lithium | |
WO2013089400A1 (fr) | Procédé pour l'extraction de lithium à partir d'une solution contenant du lithium | |
WO2023282564A1 (fr) | Procédé à haute valeur ajoutée pour la récupération de ressources à partir de boue de lithium et de boue de fluorure | |
US6261712B1 (en) | Method of reclaiming cathodic active material of lithium ion secondary battery | |
WO2022220477A1 (fr) | Méthode de production d'une solution concentrée de lithium avec un taux de récupération élevé, et méthode de production d'un composé de lithium l'utilisant | |
WO2018070726A1 (fr) | Procédé de production d'un composé de lithium | |
WO2018117771A1 (fr) | Procédé de récupération de nickel et de cobalt à partir de matière première contenant du nickel, du fer et du cobalt | |
WO2013165071A1 (fr) | Procédé de production de sulfate de manganèse monohydraté de grande pureté et sulfate de manganèse monohydraté de grande pureté produit par le procédé | |
WO2012081897A2 (fr) | Procédé de récupération et d'enrichissement de ferronickel à partir de matières premières contenant du nickel, procédé de récupération de nickel à partir de ferronickel encrichi, et procédé pour recycler la solution contenant du fer ainsi produite | |
WO2023191414A1 (fr) | Procédé de préparation d'un matériau de batterie secondaire à partir d'une masse noire | |
JP2023103929A (ja) | 廃リチウムイオン電池からリチウムを回収する方法 | |
WO2024076100A1 (fr) | Procédé de récupération d'hydroxyde de nickel et de sulfate de nickel à partir de matériaux contenant du nickel | |
WO2023182561A1 (fr) | Procédé utilisant une extraction par solvant pour récupération sélective de métal de valeur à partir de déchets de batterie secondaire au lithium | |
WO2021015378A1 (fr) | Méthode de production d'hydroxyde de lithium | |
CN113896213A (zh) | 一种锂云母除杂渣回收制备碳酸锂的工艺 | |
WO2024058441A1 (fr) | Procédé de récupération de métal du groupe du platine à partir de déchets de catalyseur en utilisant du biocyanure et du liquide ionique | |
WO2023243827A1 (fr) | Méthode de production d'une solution aqueuse contenant du nickel ou du cobalt | |
WO2022025600A1 (fr) | Procédé d'élimination sélective d'aluminium à partir d'une électrode usée et procédé de récupération d'un composant métallique à partir d'une électrode usée l'utilisant | |
CN114573006B (zh) | 镍钴锰酸锂正极材料回收提锂过程中副产物含锂粗硫酸钠的提纯及回收锂的方法 | |
WO2023080562A1 (fr) | Méthode de préparation d'hydroxyde de lithium à l'aide de carbonate de lithium et d'un composé de baryum | |
JP2000189927A (ja) | 焼却灰又は燐酸アルミニウムを含む素材からのアルミニウムと燐酸塩の分別回収法 | |
CN110195162B (zh) | 一种砷碱渣中锑、砷、碱同步浸出分离的方法 | |
WO2024147554A1 (fr) | Procédé de récupération de lithium à haut rendement à partir d'un liquide résiduaire de lithium à faible concentration et carbonate de lithium ainsi produit | |
WO2022234884A1 (fr) | Procédé de récupération de lithium à partir d'une batterie secondaire au lithium usagée en utilisant une fusion sèche | |
CN114956126A (zh) | 一种钠法磷酸铁生产过程中母液的回收利用方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 201180039418.8 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 11803831 Country of ref document: EP Kind code of ref document: A2 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2013000061 Country of ref document: CL |
|
ENP | Entry into the national phase |
Ref document number: 2013519573 Country of ref document: JP Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
REEP | Request for entry into the european phase |
Ref document number: 2011803831 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2011803831 Country of ref document: EP |